EP3983368A1 - Procédé de production de peroxydes de diacyle - Google Patents

Procédé de production de peroxydes de diacyle

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Publication number
EP3983368A1
EP3983368A1 EP20730676.2A EP20730676A EP3983368A1 EP 3983368 A1 EP3983368 A1 EP 3983368A1 EP 20730676 A EP20730676 A EP 20730676A EP 3983368 A1 EP3983368 A1 EP 3983368A1
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EP
European Patent Office
Prior art keywords
anhydride
carboxylic acid
peroxide
process according
formula
Prior art date
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Granted
Application number
EP20730676.2A
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German (de)
English (en)
Other versions
EP3983368B1 (fr
Inventor
Martinus Catharinus TAMMER
Antonie Den Braber
Carolina Anna Maria Christina Dirix
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Nouryon Chemicals International BV
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Nouryon Chemicals International BV
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/083—Preparation of carboxylic acids or their salts, halides or anhydrides from carboxylic acid anhydrides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C407/00—Preparation of peroxy compounds
    • C07C407/003—Separation; Purification; Stabilisation; Use of additives
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C407/00—Preparation of peroxy compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/41—Preparation of salts of carboxylic acids
    • C07C51/412—Preparation of salts of carboxylic acids by conversion of the acids, their salts, esters or anhydrides with the same carboxylic acid part
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/54—Preparation of carboxylic acid anhydrides
    • C07C51/56—Preparation of carboxylic acid anhydrides from organic acids, their salts, their esters or their halides, e.g. by carboxylation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • This invention relates to a process for the preparation of diacyl peroxides.
  • Diacyl peroxides have the general formula
  • Such diacyl peroxides can be prepared by reacting an excess of acid anhydride or acid chloride with alkaline solutions of hydrogen peroxide, as illustrated by the following equations:
  • [ ⁇ la2O2 does not refer to the discrete product Na2C>2, but to an equilibrium comprising H2O2 and NaOOH.
  • US 3,956,396 discloses a process to prepare a diacyl peroxide comprising reacting an anhydride and hydrogen peroxide and separating the formed product from the reaction mixture by an extraction and filtration step.
  • US 6,610,880 discloses a process for the preparation of a diacyl peroxide by reacting a mixed acid anhydride with a hydroperoxide, in which a peroxide and a carbonate monoester are formed. During work-up, the carbonate monoester decarboxylates to CO2 and an alcohol. Recycling of the alcohol requires phosgene.
  • the mixed acid anhydride is prepared by contacting a carboxylic acid with a halogen formate. This route is most relevant for making peroxides where acid chlorides are expensive or not available, such as in the case of peroxides having a hydroxy group in the molecule.
  • Acid chlorides are relatively expensive and generate chloride-containing water layers, which lead to waste waters with high salt concentration.
  • the anhydrides are even more expensive than acid chlorides and the waste stream of this process contains a high organic load - i.e. a high Chemical Oxygen Demand (COD) value - due to the formed carboxylic acid salt, and is therefore economically and environmentally unattractive.
  • COD Chemical Oxygen Demand
  • This object can be achieved by a process comprising the following steps:
  • step f) recycling at least part of the anhydride formed in step e) to step a).
  • This process produces a diacyl peroxide from an anhydride, which anhydride is obtained at least partly from the carboxylic acid side product.
  • This re-use of the carboxylic acid formed in step a) makes the route economically attractive and its effluents low in COD.
  • any additional amount of carboxylic acid that is required to form the amount of anhydride that is needed in step a) is obtained by oxidation of the corresponding aldehyde. It is therefore preferred to produce an additional amount of carboxylic acid in step d) and react it in step e) with acetic anhydride or a ketene.
  • this process does not involve the use of corrosive or volatile reactants, it increases production safety and allows production at the location in which the diacyl peroxide is eventually used (e.g. a polymerization facility).
  • Such on-site production allows peroxide production on demand, thereby minimizing storage capacities and the consequential safety measures.
  • R 1 in this formula is selected from linear and branched alkyl, cycloalkyl, aryl, and arylalkyl groups with 1 -17 carbon atoms, optionally substituted with oxygen- and/or halogen-containing substituents.
  • suitable substituents are alkoxy, chlorine, and ester substituents.
  • the number of carbon atoms is preferably 2-1 1 , even more preferably 2-8, and most preferably 3-6 carbon atoms.
  • R 1 is selected from linear or branched alkyl groups. Most preferably, R 1 is selected from the group consisting of n-propyl, n- butyl, isobutyl, 2-butyl and isopropyl groups.
  • R 2 in this formula is selected from linear and branched alkyl, cycloalkyl, aryl, and arylalkyl groups with 2-17 carbon atoms, optionally substituted with oxygen- and/or halogen-containing substituents.
  • suitable substituents are alkoxy, chlorine, and ester substituents.
  • the number of carbon atoms is preferably 2-1 1 , even more preferably 2-8, and most preferably 3-6 carbon atoms.
  • R 2 is selected from linear or branched alkyl groups. Most preferably, R 2 is selected from the group consisting of n-propyl, n- butyl, isobutyl, isobutyl, 2-butyl, and isopropyl groups.
  • Suitable symmetrical anhydrides are propionic anhydride, n-butyric anhydride, isobutyric anhydride, pivalic anhydride, n-valeric anhydride, isovaleric anhydride, 2-methylbutyric anhydride, 2-methylpentanoic anhydride, 2-methylhexanoic anhydride, 2-methylheptanoic anhydride, 2-ethylbutyric anhydride, caproic anhydride, caprylic anhydride, isocaproic anhydride, n-heptanoic anhydride, nonanoic anhydride, isononanoic anhydride, 3,5,5-trimethylhexanoic anhydride, 2-propylheptanoic anhydride, decanoic anhydride, neodecanoic anhydride, undecanoic anhydride, neoheptanoic anhydride, lauric anhydride, tridecanoic anhydride, 2-e
  • suitable mixtures of symmetrical anhydrides are the mixture of isobutyric anhydride and 2-methylbutyric anhydride, the mixture of isobutyric anhydride and 2-methylpentanoic anhydride, the mixture of 2-methylbutyric anhydride and isovaleric anhydride, and the mixture of 2-methylbutyric anhydride and valeric anhydride.
  • Asymmetrical anhydrides are usually available as a mixture of asymmetrical and symmetrical anhydrides. This is because asymmetrical anhydrides are usually obtained by reacting a mixture of acids with, e.g., acetic anhydride. This leads to a mixture of anhydrides, including an asymmetrical and at least one symmetrical anhydride. Such mixtures of anhydrides can be used in the process of the present invention.
  • Suitable asymmetrical anhydrides are isobutyric-2- methylbutyric anhydride, which is preferably present as admixture with isobutyric anhydride and 2-methylbutyric anhydride; isobutyric-acetic anhydride, which is preferably present as admixture with isobutyric anhydride and acetic anhydride; propionic-isobutyric anhydride, which is preferably present as admixture with propionic anhydride and isobutyric anhydride; 2-methylbutyric-valeric anhydride, which is preferably present as admixture with 2-methylbutyric anhydride and valeric anhydride; and butyric-valeric anhydride, which is preferably present as admixture with butyric anhydride and valeric anhydride.
  • the anhydride is symmetrical. More preferred symmetrical anhydrides are isobutyric anhydride, 2-methylbutyric anhydride, 2-methylhexanoic anhydride, 2-propylheptanoic anhydride, isononanoic anhydride, cyclohexanecarboxylic anhydride, 2-ethylhexanoic anhydride, caprylic anhydride, n-valeric anhydride, isovaleric anhydride, caproic anhydride, and lauric anhydride. Most preferred is isobutyric anhydride. Step a) is performed at temperatures in the range -10 to 70°C, more preferably 0 to 40°C, most preferably 5 to 30°C.
  • the molar ratio H2O2 : anhydride is preferably in the range 0.40:1 to 1.0:1 , more preferably 0.45:1 to 0.70:1 , and most preferably 0.50:1 to 0.60:1.
  • the pH of the water phase during this reaction is preferably at least 6, more preferably at least 7, and most preferably at least 9.
  • Suitable bases that may be added to reach this pH include oxides, hydroxides, bicarbonates, carbonates, (hydro)phosphates, and carboxylates of magnesium, lithium, sodium, potassium, or calcium.
  • the base is preferably added in amounts of 50-200 mol%, more preferably 70- 140 mol%, and most preferably 90-120 mol%, relative to anhydride.
  • the reaction does not require the presence of a solvent.
  • a solvent can be pre-charged or dosed to the reaction mixture during the reaction.
  • Suitable solvents are alkanes, chloroalkanes, esters, ethers, amides, and ketones.
  • Preferred solvents are (mixtures of) alkanes, such as isododecane, Spirdane®, Isopar® mineral oils; esters like ethyl acetate, methyl acetate, ethylene glycol dibenzoate, dibutyl maleate, di-isononyl-1 ,2-cyclohexanedicarboxylate (DINCH), or 2,2,4-trimethylpentanediol diisobutyrate (TXIB); and phthalates, such as dimethyl phthalate or dioctyl terephthalate.
  • alkanes such as isododecane, Spirdane®, Isopar® mineral oils
  • esters like ethyl acetate, methyl acetate, ethylene glycol dibenzoate, dibutyl maleate, di-isononyl-1 ,2-cyclohexanedicarboxylate (DINCH), or 2,2,4-trimethylpentan
  • the reaction mixture resulting from step a) is a biphasic mixture, containing an aqueous and an organic phase.
  • step b) the carboxylic acid is extracted or separated from the mixture in the form of its carboxylic acid salt or adduct.
  • the formation of said salt or adduct requires the presence of a base. If no base was present during step a) or if the amount of base added during step a) is insufficient to transform the majority of carboxylic acid into the corresponding salt or adduct, a base or an additional amount of base may be added in step b). If the amount of base present in the mixture resulting from step a) is sufficient to transform the majority of carboxylic acid into the corresponding salt or adduct, then no additional amount of base needs to be added in step b).
  • Suitable bases are alkylated amines, oxides, hydroxides, bicarbonates, carbonates, and carboxylates of magnesium, lithium, sodium, potassium, or calcium. These bases will deprotonate the carboxylic acid, thereby forming a water-soluble salt that ends up in the aqueous phase. The organic phase and the aqueous phase are subsequently separated.
  • Suitable bases are solid materials with basic functions that are able to capture the carboxylic acid, thereby forming an adduct.
  • solid materials are basic ion exchange resins such as poly(styrene-co- vinylbenzylamine-co-divinylbenzene), N- ⁇ 2-[bis(2-aminoethyl)amino]ethyl ⁇ aminomethyl-polystyrene, diethylaminomethyl-polystyrene, dimethylamino methylated copolymers of styrene and divinylbenzene, polymer-bound morpholine, poly(4-vinylpyridine), zeolites or mesoporous silicas containing alkylamine groups like 3-aminopropylsilyl-functionalized SBA-15 silica, polymeric amines, and mixtures of one or more of these materials.
  • the formed adduct can be removed from the reaction mixture by filtration.
  • the organic phase containing the diacyl peroxide may be purified and/or dried. Purification can be performed by washing with water, optionally containing salts, base, or acid, and/or filtration over, e.g., carbon black or diatomaceous earth. Drying can be performed by using a drying salt like MgSC>4 or Na2SC>4 or by using an air or vacuum drying step. If the diacyl peroxide is to be emulsified in water, a drying step can be dispensed with. In step c), the carboxylic acid is liberated by, for instance,
  • Preferred acids for acidifying and protonating the carboxylic acid are acids with a pKa below 3, such as H2SO4, HCI, NaHSC>4, KHSO4, and the like. Most preferably H2SO4 is used. If H2SO4 is used, it is preferably added as a 90-96 wt% solution. Acidification is preferably performed to a pH below 6, more preferably below 4.5, and most preferably below 3. The resulting pH is preferably not lower than 1.
  • a small amount of a reducing agent such as sulfite and/or iodide, may be added to the aqueous phase in order to decompose peroxide residues.
  • a thermal treatment e.g. at 20-80°C can be applied in order to decompose any diacyl peroxide residues.
  • the organic layer containing the carboxylic acid is then separated from any aqueous, salt-containing layer. Separation can be performed by gravity, using conventional separation equipment, such as a liquid/liquid separator, a centrifuge, a (pulsed and or packed) counter current column, (a combination of) mixer settlers, or a continuous (plate) separator.
  • separation equipment such as a liquid/liquid separator, a centrifuge, a (pulsed and or packed) counter current column, (a combination of) mixer settlers, or a continuous (plate) separator.
  • the separation can be facilitated by salting out the organic liquid phase with a concentrated salt solution, e.g. a 20-30 wt% NaCI, NaHSC>4, KHSO4, Na2SC>4, or K2SO4 solution.
  • a concentrated salt solution e.g. a 20-30 wt% NaCI, NaHSC>4, KHSO4, Na2SC>4, or K2SO4 solution.
  • the salt reduces the solubility of the carboxylic acid in the aqueous liquid phase.
  • This extraction can be performed in any suitable device, such as a reactor, centrifuge, or mixer-settler.
  • a residual amount of the acid will remain dissolved in the aqueous layer. This residual amount can be recovered by adsorption, (azeotropic) distillation, or extraction.
  • a salt e.g. sodium sulfate
  • liberation of the carboxylic acid is achieved by electrochemical membrane separation. Examples of electrochemical membrane separation techniques are membrane electrolysis and bipolar membrane electrodialysis (BPM). BPM is the preferred electrochemical membrane separation method.
  • Electrochemical membrane separation leads to splitting of the metal carboxylate in carboxylic acid and metal hydroxide (e.g. NaOH or KOH) and separation of both species. It thus leads to (i) a carboxylic acid-containing mixture and (ii) a NaOH or KOH solution, separated by a membrane.
  • carboxylic acid and metal hydroxide e.g. NaOH or KOH
  • the NaOH or KOH solution can be re-used in the process of the present invention, for instance in step a).
  • the carboxylic acid-containing mixture can be a biphasic mixture of two liquid phases or a homogeneous mixture. If a homogeneous mixture is formed under the electrochemical membrane separation conditions (generally 40-50°C), cooling of the mixture to temperatures below about 30°C and/or the addition of salt will ensure that a biphasic mixture will be formed. The organic liquid layer of this biphasic carboxylic acid-containing mixture can then be separated from the aqueous layer by gravity or by using equipment like a centrifuge.
  • the carboxylic acid-containing organic phase is optionally purified to remove volatiles like alcohols, ketones, alkenes and water before it is used in step e). These volatiles can be removed by adsorption, distillation, or drying with salt, molecular sieves, etc. Distillation is the preferred way of purification.
  • the distillation preferably involves two product collection stages, one to collect impurities like alcohols, and another to collect the remaining water, optionally as an azeotrope with the carboxylic acid.
  • step e in particular the reaction with acetic anhydride, is advantageously performed in a reactive distillation column that is fed in the middle sections with the carboxylic acid and the acetic anhydride.
  • the product anhydride is drawn from the bottom of the column and the product acetic acid is collected from the top of the column.
  • An alternative method is to produce the anhydride in a stirred reactor surmounted by a distillation column. This allows the acetic acid to be distilled when formed in order to shift the equilibrium.
  • US 2005/014974 discloses a process to prepare isobutyric anhydride by reacting acetic anhydride with isobutyric acid and containing a step of distilling of the acetic acid as formed.
  • the distillation column is preferably sufficiently efficient to get high purity acetic acid.
  • the efficiency of the column is preferably at least 8 theoretical plates. High purity acetic acid can be sold and/or used for various purposes.
  • a catalyst may be used in step e), although it is preferred to perform the reaction in the absence of catalyst.
  • suitable catalysts are oxides, hydroxides, bicarbonates, carbonates, and carboxylates of magnesium, lithium, sodium, potassium, or calcium.
  • the molar ratio of carboxylic acid to acetic anhydride is preferably in the range 0.5:1 to 5:1 , more preferably 1.5:1 -2.2:1 , most preferably 1.8:1 to 2.2:1 . A slight excess of carboxylic acid relative to acetic anhydride might be used.
  • This anhydride can then be used again in step a).
  • the carboxylic acid that is used in step e) is obtained from two or three sources.
  • the first source is the carboxylic acid that is liberated in step c).
  • the second source is the carboxylic acid obtained by oxidation of the corresponding aldehyde in accordance with step d), as described below.
  • the third source is an additional amount of carboxylic acid obtained in any other way.
  • oxygen source for step d air is preferably used, although pure oxygen, oxygen-enriched, or oxygen-lean air may also be applied.
  • the oxygen source can be added to the reaction mixture by feeding it as a gas to the reactor, preferably using a sparger.
  • step d) is preferably performed at a temperature in the range of 0-70°C, more preferably in the range 10-60°C, and most preferably in the range 20-55°C.
  • Atmospheric pressure is preferably used; at lower pressure the aldehyde may evaporate, which is undesired.
  • a catalyst may optionally be used.
  • Very good catalysts which not only accelerate oxidation but also increase the yield of acid, are platinum black and ferric salts.
  • Cerium, nickel, lead, copper and cobalt salts are also useful, particularly their carboxylic acid salts.
  • the catalyst may be added in amounts of 0 to 20 mol% relative to aldehyde, more preferably 0-5 mol%, and most preferably 0-2 mol%.
  • diacyl peroxides which can particularly suitably be produced by this process are di-2-methylbutyryl peroxide, di-iso-valeryl peroxide, di-n-valeryl peroxide, di-n-caproyl peroxide, di-2- methylhexanoyl peroxide, di-2-propylheptanoyl peroxide, di-isononanoyl peroxide, di-cyclohexylcarbonyl anhydride, di-2-ethylhexanoyl anhydride, acetyl- isobutyryl peroxide, propionyl-isobutyryl peroxide, and di-isobutyryl peroxide. The most preferred is di-isobutyryl
  • Steps that are preferably performed in continuous mode are reactive distillation to make the anhydride in step e) and isolation and purification of the carboxylic acid in step c).
  • step e a batch reaction to the diacyl peroxide in step a), followed by a batch separation and continuous purification of carboxylic acid and continuous reactive distillation towards the anhydride in step e),
  • step e a batch reaction to diacyl peroxide and separation of the product, followed by a continuous mode purification of carboxylic acid and continuous reactive distillation to the anhydride in step e).
  • the aqueous phase was allowed to separate by gravity and was subsequently removed.
  • the organic layer - containing 62.6 wt% di-n-butyryl peroxide - was dried with MgSC>4 -2H20 and filtered over a G3 glass filter.
  • the aqueous phase (241 g) was stirred at 0-5°C with 18.3 g Spirdane® D60 to extract residual peroxide and the layers were allowed to separate.
  • H2SO4 (26.8 g, 96 wt%) was subsequently added to the water layer, resulting in a temperature increase to 27°C.
  • a 215.4 g water layer and a 51 .6 g organic layer were obtained, which layers were separated.
  • the organic compounds in said organic layer consisted for more than 99 wt% of butyric acid.
  • n-butyric acid was mixed with n-butyric acid from another source (in this case, from Sigma Aldrich) and then reacted with acetic anhydride in a molar ratio n- butyric acid:acetic anhydride of 2:1 .05 and heated to distill the acetic acid at ⁇ 400 mbar and 120°C to obtain n-butyric anhydride as the residue.
  • This anhydride was then recycled to the first step in which it was reacted with H2O2.
  • the water layer was allowed to settle by gravity and was subsequently removed.
  • the organic layer contained 70.9 wt% di-isobutyryl peroxide, corresponding to a yield of 94%, calculated on anhydride.
  • the water layer contained about 24 wt% of sodium isobutyrate.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de production d'un peroxyde de diacyle comprenant la réaction d'un anhydride avec du peroxyde d'hydrogène, l'élimination de l'acide carboxylique formé, la production d'un anhydride à partir dudit acide carboxylique et le recyclage de l'anhydride dans le procédé.
EP20730676.2A 2019-06-12 2020-06-11 Procédé de production de péroxydes de diacyle Active EP3983368B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP19179620 2019-06-12
PCT/EP2020/066227 WO2020249688A1 (fr) 2019-06-12 2020-06-11 Procédé de production de peroxydes de diacyle

Publications (2)

Publication Number Publication Date
EP3983368A1 true EP3983368A1 (fr) 2022-04-20
EP3983368B1 EP3983368B1 (fr) 2023-08-02

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US (1) US11976035B2 (fr)
EP (1) EP3983368B1 (fr)
JP (1) JP7336541B2 (fr)
ES (1) ES2963357T3 (fr)
HU (1) HUE063679T2 (fr)
WO (1) WO2020249688A1 (fr)

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CN114805057B (zh) * 2022-06-10 2024-02-02 福建技术师范学院 一种隔壁反应精馏生产丁酸酐的生产方法

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US11976035B2 (en) 2024-05-07
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JP7336541B2 (ja) 2023-08-31
JP2022536700A (ja) 2022-08-18
BR112021024874A2 (pt) 2022-01-25
US20220251038A1 (en) 2022-08-11
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